Combustible fuel and apparatus and process for creating the same

ABSTRACT

Features for an aqueous reactor include a field generator. The field generator includes a series of parallel conductive plates including a series of intermediate neutral plates. The intermediate neutral plates are arranged in interleaved sets between an anode and a cathode. Other features of the aqueous reactor may include a sealed reaction vessel, fluid circulation manifold, electrical power modulator, vacuum port, and barrier membrane. Methods of using the field generator include immersion in an electrolyte solution and application of an external voltage and vacuum to generate hydrogen and oxygen gases. The reactor and related components can be arranged to produce gaseous fuel or liquid fuel. In one use, a mixture of a carbon based material and a liquid hydrocarbon is added. The preferred carbon based material is powdered coal.

CROSS REFERENCE TO RELATED PATENT APPLICATIONS

This application claims priority to and is continuation-in-part of U.S.non-provisional application Ser. No. 16/120,427 filed Sep. 3, 2018,which is a divisional application of U.S. non-provisional applicationSer. No. 14/119,871 filed Nov. 23, 2013 granted as U.S. Pat. No.10,066,304 on Sep. 4, 2018, which is a national application of PatentCooperation Treaty application PCT/US2012/039211 filed May 23, 2012, andclaims priority thereto and to U.S. Provisional Application Ser. No.61/489,059 filed May 23, 2011 and 61/566,554 filed Dec. 2, 2011, all ofwhich are incorporated by reference herein in their entirety.

TECHNOLOGICAL FIELD

The present technology relates to the field of combustible fuels and theprocesses and apparatus needed to efficiently create combustible fuels.

BACKGROUND

Electrolysis of water to generate hydrogen and oxygen under an appliedelectric field using various forms of apparatus is well known. Alsoknown are HHO generators which use electrolysis to transform water intoits component parts but not to separate the hydrogen and oxygen oncereleased. So too is the reformation of hydrocarbons into hydrogen gas orhydrogen-enhanced gas. But more practical processes for the creation ofsuch fuels are needed.

SUMMARY

The present technology is directed to aspects and use of an aqueousreactor using an applied electric field to initiate or sustain areaction by which a clean burning fuel is created.

In a first separate aspect of the present technology, an electric fieldgenerator is provided for use in the aqueous reactor. The electric fieldgenerator comprises a series of electrically conductive parallelspaced-apart plates in an array. One or more first plates of the array,located at a first end of the array, is connected to a source of appliedelectrical power of a first polarity (e.g., positive or negative). Oneor more second plates of the array, located at an end of the arrayopposite to the first end, is connected to a source of appliedelectrical power of a second polarity, opposite to the first polarity. Aset of third plates of the array are preferably interposed between theone or more first plates (herein called the “cathode plates”) and theone or more second plates (herein called the “anode plates”). The thirdplates are preferably unconnected to any source of applied electricalpower, to serve as neutral electrodes. The third plates may be arrangedin subsets each comprising at least three plates of the array. All ofthe plates within each of the subsets may be electrically interconnectedwith each other.

The foregoing technology may further include the subsets beingunconnected to other ones of the subsets except through the field in theaqueous reactor, the cathode plates, and the anode plates. The subsetsare preferably arranged so that each subset includes at least one platethat is interposed between two plates of an adjacent subset, of thecathode plates, or of the anode plates, and also includes at least twoplates disposed around (i.e., having interposed there between) one plateof another adjacent subset, of the cathode plates, or of the anodeplates. Such an arrangement of plate subsets is referred to herein as“interleaving” or “interleaved.” A subset consisting of three plates maybe referred to herein as a “triplet.”

The foregoing technology may further include the anode and cathodeplates coupled to opposite poles of an electrical power modulator. Theelectric power modulator may supply a step modulated or ladder switcheddirect current waveform to the field generator at less than 100% dutycycle. For example, the power modulator may supply a step modulateddirect current waveform at a 50% duty cycle. The waveform may becharacterized by having a relatively low peak voltage, for example abouta peak voltage in the range of 14-24 Volts, and alternating between zeroand the peak voltage. However, the technology is not limited to a peakvoltage in this range.

The foregoing technology may include an aqueous working fluid to producehydrogen and oxygen gases such as HHO applied to a field generator,reaction vessel and/or other aspects as described above. The fieldgenerator is preferably immersed in the working fluid and electric powerapplied to opposite poles of the field generator as described above. Theaqueous working fluid is preferably comprised of a solution of puredistilled water and a hydroxide salt, for example, potassium hydroxide(KOH). The hydroxide salt functions as an electrolyte and is notconsumed. The distilled water is electrolyzed to hydrogen and oxygen attemps preferably between about 115.degree. F. and 130.degree. F. Make upwater may be added as the water is consumed to maintain a constant waterlevel. Non-distilled water can preferably be used but may causeincreased corrosion or fouling of the apparatus.

The foregoing technology may further include a non-electricallyconductive and substantially gas-impermeable barrier membrane, forexample a polymer film or sheet material, extending above the level ofthe liquid between the anode and the cathode. The membrane forms abarrier to prevent the comingling of produced gases from the anode andthe cathode.

A mixture of hydrogen and oxygen gas may be drawn out of the reactionvessel using a vacuum pump. The output of the reactor can be varied bythe pressure and temperature maintained within the vessel duringoperation. Thus, it is advantageous to maintain a vacuum in the reactionvessel in the range of about 0.2 to 0.9 atmospheres, and more preferablyabout 0.2-0.5 atmospheres while the temperature of the working fluid ismaintained within a defined range of preferably between 115.degree. F.to 130.degree. F., using fluid recirculation. The vacuum and temperatureare balanced to keep the water from boiling or reaching a point wheresubstantial water is vaporized in the process.

The foregoing technology can alternatively be employed to include anaqueous working fluid applied to the field generator, reaction vesseland/or other aspects as described above to produce a liquid hydrocarbonfuel from a solution containing carbon based material. The carbon basedmaterial, such as preferably a carbon or coal powder, is dispersed insuspension in an aqueous working fluid as described herein above. Theaqueous working fluid preferably includes an initial charge of ahydrocarbon fuel, such as kerosene, diesel, or other such fuels down toand including a molecular weight of gasoline with the carbon basedmaterial maintained in suspension.

As discussed above, the output of the reactor can be varied by thepressure and temperature maintained within the vessel during operation.The temperature of the working fluid is maintained within a definedrange of between 180.degree. F. to 200.degree. F., using fluidrecirculation without pressure, again to avoid boiling or thesubstantial production of water vapor. Under pressure, the upper end ofthe temperature can be raised accordingly.

In forming hydrocarbon fuel from carbon based material, conditions maybe adjusted empirically to insure reduction of the in-processhydrocarbon fuel to have reduced average molecular weight. For example,most hydrocarbons may be reformed to a hydrocarbon having eight or fewercarbon atoms.

In a further separate aspect of the present technology, the anode andcathode plates include a pattern of holes which extend acrosssubstantially the full plate to provide an open area which is greaterthan the occupied area of the plate. The nominal size of the anode andcathode plates is similar to the size of the neutral plates. All platesare preferably made from highly conductive metal, such ascopper-tungsten to reduce heat and insure good conductivity. The platesare also plated with a catalyst such as nickel interactive in theelectrolysis process. Palladium, platinum or other catalysts may also beuseful in facilitating a desired reaction at lower temperatures in theelectrolysis.

The foregoing technology may further include any of the foregoingaspects can be combined to greater result.

Accordingly, objects of the present technology may include providingnovel features and combinations to enhance operation of an aqueousreactor using an applied electric field to initiate or sustain achemical reaction or the creation of a plasma in the reactor, forexample generation of hydrogen and oxygen gas from water, orhydroxylation/hydrogenation of carbon or organic compounds, the fueloutput from such technology and methods for using such features andcombinations. Other and further objects and advantages will appearhereinafter.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic diagram illustrating one embodiment of the presenttechnology relating to a field generator.

FIG. 2 is a block diagram illustrating an arrangement of neutralsubsets, cathode plates and anode plates for an embodiment of a fieldgenerator.

FIG. 3 is a plan view showing an example of a plate for use in a fieldgenerator.

FIGS. 4A-4B are schematic diagrams illustrating alternativeconfigurations for plates in a field generator.

FIG. 5 is a perspective cut away view of an aqueous reactorincorporating a field generator.

FIG. 6A is a schematic block diagram of an apparatus including anaqueous reactor to generate hydrogen and oxygen from an aqueous workingfluid.

FIG. 6B is a detail schematic showing an alternative configuration ofthe aqueous reactor including an intermediate barrier for gasseparation.

FIG. 7 is a flow chart showing an example of a method for operating anaqueous reactor to generate hydrogen and oxygen from an aqueous workingfluid.

FIG. 8 is a flow chart showing addition operations that may be used withthe method shown in FIG. 7.

FIG. 9 is a schematic illustrating an embodiment of an alternativeconfiguration of the technology.

FIG. 10 is a plan view of an embodiment of an anode or cathode plate.

FIG. 11 is a graphical representation of a voltage signal as a functionof time as measured at test point 1 of FIG. 6A.

FIG. 12 is a graphical representation of a current signal as a functionof time as measured at test point 1 of FIG. 6A.

FIG. 13 is a graphical representation of a voltage signal as a functionof time as measured at test point (TP) 2 of FIG. 6A.

FIG. 14 is a graphical representation of a current signal as a functionof time as measured at TP 2 of FIG. 6A.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT

With reference to FIG. 1, a field generator 100 for use in an aqueousreactor preferably comprises an array 102 of electrically conductiveparallel spaced-apart plates 104 a-104 j supported by a non-electricallyconductive framework or member 106. The array of plates 102 may compriseone or more cathode plates 104 a, 104 c (collectively, 108) at a firstend of the array, one or more anode plates 104 h, 104 j (collectively,110) at a second end of the array 102 opposite to the first end. Thearray of plates may further comprise a plurality of neutral plates 104b, 104 d-g, 104 i interposed between the cathode plates 108 and theanode plates 110. The neutral plates 104 b, 104 d-g, 104 i may bearranged in interleaved neutral subsets 112, 114 each comprising atleast three electrically connected plates. As mentioned above,interleaving of the neutral subsets means that each subset 112, 114includes at least one plate (e.g., 104 b, 104 f, 104 i) that isinterposed between two plates of an adjacent subset, of the cathodeplates, or of the anode plates, and also includes at least two plates(e.g., 104 d and 104 f of subset 112, or 104 e and 104 g of subset 114)disposed around one plate of another adjacent subset, of the cathodeplates, or of the anode plates. Each of the neutral subsets 112, 114 maybe electrically isolated from other ones of the neutral subsets, fromthe cathode plates, and from the anode plates. For example, each of theneutral subsets 112, 114 may be electrically isolated from every otherone of the neutral subsets.

In a low power mode, the cathode plates 108 may be configured forconnecting to a negative polarity source of applied electrical power,for generating hydrogen. The anode plates 110 may be configured forconnecting to a positive polarity source of applied electrical power forgenerating oxygen. The neutral subsets are not connected to any sourceof electrical power.

The plates 104 a-j are preferably copper-tungsten or other highlyconductive material. For the creation of hydrocarbon based fuels, thehighly conductive material includes a catalytic surface such as isprovided by nickel-plating. The nickel-plated surface treatment of theconductive plates has been observed to have a catalytic effect on theoperation of the aqueous reactor.

The plates 104 a-j are preferably substantially planar and ofsubstantially uniform thickness “t”. It is believed desirable to makethe plates thick enough to be durable and rigid during operation of thereactor, and optimal thickness may therefore depend on the selectedplate material and plate mounting details. If copper-tungsten is used,the plates are advantageously 0.125″ to avoid accidental bending of thesoft material. The plates in the array will preferably be spacedsubstantially uniformly apart a distance “d” in a range of about 0.125inches from one another. Depending upon the material utilized for theplates, an advantageous surface roughness is preferred of about 400 toabout 1200 microns, and more preferably between about 500 and 1000microns. Further aspects of the field generator “plate” are described inconnection with FIGS. 3 and 10 below.

The non-electrically conductive framework or member 106 comprises edgesupports spaced around a periphery of the plates. Edge supports arebelieved advantageous to ensure that each plate remains in place duringoperation. A support member preferably includes other features, forexample nozzles 106 for a recirculation manifold as discussed herein. Inan embodiment, plate edges were supported by slots formed in blocks of apolymer material, to support the array around a periphery of the plateedges. However, any suitable support structure may be used.

Although the field generator is not limited to a particular number ofthe plates 104 a-j, in one embodiment the apparatus preferably comprisesnot less than nine and not more than 48 neutral plates. An array havingproperties as described herein is believed to be effective, and perhapsoptimally effective, using twenty-five total plates comprised of twocathode plates 202, two anode plates 204, and 21 neutral plates dividedinto seven triplets 206 a-g. Such an array 200 is illustrated in ahighly schematic form in FIG. 2, which is not to scale and is drawnmainly to illustrate an example of an interleaved plate topology for afield generator 200. The illustrated manner of connecting plates in atriplet, anode or cathode is highly schematic, and should not beunderstood as illustrating or suggesting an actual physicalconfiguration, apart from the illustrated and described topologicalaspects.

Each of the neutral subsets 206 a-g is preferably comprised an oddnumber of plates, for example, three or five. Three plates per neutralsubset (i.e., a triplet) is believed advantageous, although any oddnumber of three or greater enables interleaving of the neutral subsets,as clearly depicted in FIGS. 1 and 2. Interleaving is believed to beadvantageous to operation of the field generator for electrolysis ofwater and other reactions, at least for use with the applied electricalpower waveforms as described herein. In the interleaved embodiment shownin FIG. 2, the cathode plates 202 are interleaved with a first neutraltriplet 206 a, and the anode plates 204 are interleaved with a lastneutral triplet 206 g. The first and last triplets 206 a, 206 g areinterleaved with their adjoining triplets 206 b, 206 f, respectively.The intermediate triplets 206 b-f are each interleaved with an adjoiningtriplet. FIG. 1 shows a similar arrangement.

The array 200 may comprise an odd or even number of neutral subsets suchas the triplets 206 a-g. An odd number of neutral subsets is believedadvantageous, at least for use with the applied electrical powerwaveforms as described herein.

FIG. 3 shows a plan view and dimensions for an example of a plate 300used to construct a field generator as described herein. The plate 300as shown is employed for the neutral plates 104 b, 104 d-g, 104 i ofFIG. 1 and FIG. 10. Highly conductive materials may be suitable, forexample, copper, nickel-plated copper, nickel, platinum or palladiumplated metals, or graphite. Other metals have also been used. Anystructural conductive material may be used that is either coated or willnot be appreciably corroded by the working fluid of the aqueous reactorduring use. Any surface material selected may have an effect on theoperation of the field generator. There appears to be a catalytic effectobserved when nickel plating covers the plates 104 a-j in theelectrolytic process. Additionally, the presence of nickel, palladium,platinum or other catalysts may be helpful in facilitating a desiredreaction at lower temperatures. Various surface treatments can enhanceoperation of the field generator, although robust hydrolysis of water ina potassium hydroxide solution was even observed using untreated 316 Lstainless steel.

The plate 300 may be characterized by opposing generally parallelprimary surfaces. One of these surfaces 302 is shown in the plan view ofFIG. 3. The opposite surface of plate 300 comprises the second surface.This characteristic enables construction of a field generator asdescribed in connection with FIGS. 1 and 2. These primary surfaces arenot necessarily flat and planar, and may be contoured so long asmaintaining a generally parallel orientation with respect to theadjacent surface of its closest neighboring plate.

The dimensions and shape shown in FIG. 3 are provided by way of exampleonly, and not by limitation. The depicted dimensions and shape arebelieved useful for, but not critical to, construction of a fieldgenerator. The plate 300 includes a central hole 304 to accommodate anon-conductive support member used to support plates in the fieldgenerator. Additional holes 304 may be incorporated to accommodateadditional non-conductive support members to align multiple plates withone another. The plate 300 could preferably include any number of holesor cutouts and may be made in a variety of shapes. The plate 300 mayinclude a tab 306 for use as an electrical connector to an adjacentplate, to an external power source, or both. As used herein, “plate” isnot limited to generally planar components, or to components made ofplate stock. Instead, a “plate” should be understood to be preferablygenerally flat, contoured or folded, with any number of through holesand formed of any suitable material. For example, a grid or wire meshmaterial, so long as sufficiently rigid to hold its shape in operation,may be configured as a “plate” in the field generator as describedherein.

Substantially all stated above in reference to plate 300 applies to theanode plates 104 h, 104 j and cathode plates 104 a, 104 c. In certain ofthe processes described, the anode plates 104 h, 104 j and cathodeplates 104 a, 104 c have found further efficiency using holes in theseplates. This is particularly true for the hydrocarbon and carbonconversion process. Such anode and cathode plates are also schematicallyillustrated in FIG. 10. The representative plate 310 includes a patternof holes 312. This is but one of an almost infinite pattern of holesthat might be applied. The object is to significantly cover the plate310 with the holes 312. The employment of this type of plate for theanodes and cathodes has been found to cut power requirements andincrease production of gas, which is evolved and released more rapidlyfrom the plate due to the increased edges surrounding such holes. Inthis specific embodiment, a plate of copper-tungsten plated with nickeland having a nominal height/width/depth of 6″.times.6″.times.⅛″ isperforated uniformly before plating with holes 5/16″ square. The holes312 are spaced apart ⅛″, giving a hole center-to-center distance betweenadjacent holes of 7/16″. A slightly wider structural border 314 extendsabout the periphery of the plate 310.

Although plates 300, 310 may be generally flat or planar, the fieldgenerator is not limited to use of planar plate elements. For example,contouring or folding may be used to increase surface area of a plate,while maintaining a generally parallel relationship with an adjacentplate. FIG. 4A shows a top view of two adjacent contoured plates 402,404 in a configuration 400 wherein each of the plates 402, 404 includesrespective contoured surfaces 406, 408 maintaining collinear (or nearcollinear) normals for substantially their entire respective extents. Adrawback of this configuration is that in an array made up of plates ofequal area, exact parallelism cannot be maintained between adjacentplates without individually contouring each plate. This can be avoidedby using an alternative configuration 450, shown in FIG. 4B, in whichfolded adjacent plates 452, 456 present multiple folds definingrespective virtual surfaces 456, 458, which are substantially parallel.Adjacent plates 452, 456 may therefore share substantially the same oridentical contoured geometries while still providing an aspect ofparallelism between adjacent plates. The alternative configurations 400,450 are currently untested and may not, on balance, be advantageous overflat plates. Advantages of flat plates include simplicity offabrication, lower cost, easily achieved parallelism and less resistanceto fluid flow between adjacent plates.

FIG. 5 shows an example of a field generator 502 assembled into anaqueous reactor 500. The reactor 500 includes a substantially closedvessel or container 504, constructed for holding a liquid working fluidso as to immerse the field generator 502. The field generator 502 maycomprise an array of plates, for example, the neutral plate 300 as shownin FIG. 3 and the anode/cathode plate 310 shown in FIG. 10, supported bya non-electrically conductive framework 506. A cylindricalnon-conductive support member (not shown) may pass through a centralhole 507 in the plates to secure the plates to the supporting framework.The plates may be connected to provide cathode plate sets, anode platesets, and neutral sets as described herein, using connectors (not shown)placed across selected connecting tabs at the upper end of the generator502. During operation, the liquid level in the container 504 may bemaintained below the level of the plate connecting tabs, for example thetab 508 that is connected to an electrical cable 510 supplyingelectrical power to the field generator 502. A complementary electricalcable, not visible in this view, may similarly be connected to a plateof opposite polarity located at an opposite end of the array 502.

The cable 510 or its complement may be passed through a wall of thecontainer 504 using a feed-through 512 designed to maintain a seal.Where power straps are employed in the bath to distribute current, theytoo may be nickel coated and of a highly conductive material to reduceheat build-up and provide more catalytic surface area. The container 504may be substantially sealed except for control inlet and outlet ports,examples of which are discussed below. In the illustrated unit 500, anO-ring seal 514 is disposed around a base 516; however, any suitableseal may be used.

A liquid inlet 518 and outlet 520 in the base 516 may be provided forconnecting to a recirculation system, which may comprise a pump, heatexchanger, and connecting lines. The recirculation system, among otherthings, may circulate the working fluid through an array of nozzles inthe base 516. The nozzles preferably inject the working fluid in betweenindividual plates in the field generator 502. Fluid injection betweenthe plates is believed helpful for enhancing fluid movement, heattransfer and mixing between the plates, and to help strip accumulatedgas bubbles from the plate surfaces. Upper ports include one or moreliquid addition ports 524 and 526 for addition and make-up of workingfluid constituents, and a solids entry/inspection port 528.

An aqueous reactor as described above may be used in an apparatus 600for reacting an aqueous working fluid in an electric field, furtheraspects of which are illustrated in FIG. 6A. The apparatus 600preferably includes a source 602 of applied electrical power connectedto the cathode plates and anode plates of an aqueous reactor 601, aspreviously described. The power source 602 preferably comprises a pulsewidth modulator 604, also called a waveform generator, which preferablyincludes a programmable logic controller (PLC) or electronic controlunit (ECU) 611. Preferably, the wave form generator 604 can supply aDirect Current (DC) drive signal 606 to a field winding 608 of athree-phase alternator 610. The DC drive signal preferably has a dutycycle in a range of about 10% to 90%, a frequency in a range of about500 Hz to 32 kHz, and a peak voltage in a range of about 5 to 50 V. Morepreferably, the DC drive signal 606 has a duty cycle of about 50% and apeak voltage of about 14-24 V, depending on the size of the fieldgenerator 603. When step switched and pulse switched, the 50% duty cycleprovides a drive signal for the field generator at 25% of the currentdraw at the source 604.

For example, a PLC or other source 611 preferably generates a drivesignal 605 at a first frequency and first duty cycle to drive aswitching device 613, such as a solid state relay. The source 611preferably provides a pulse width modulated (PWM) power signal 607 at asecond frequency and second duty cycle to an input of the switchingdevice 613. In an embodiment, the first and second duty cycles couldpreferably be equal and set to 50% or about 50%, and the secondfrequency may be much higher than the first frequency, for example atleast ten times greater. For example, in an embodiment, a firstfrequency of about 500 Hz to 1 kHz and more preferably about 800 Hz maybe used for the drive signal 605 at duty cycle of 50% at 24 V, and asecond frequency of 60 kHz at 12 V, 50% duty cycle, may be used for thePWM power signal 607. The switching device therefore generates the DCdrive signal 606 having a frequency and duty cycle equal to the firstfrequency and duty cycle. A capacitor 609 is preferably connected acrossthe input and output terminals of the switching device 613 to filter outthe higher second frequency and reduce current draw from the source 611.The peak voltage and power of the drive signal 606 is determined by thepower signal 607, in this example 12 V.

By applying the drive signal 606 to the field winding 608 of thethree-phase alternator 610, on/off switch may be accomplished bybuilding and collapsing a magnetic field, instead of junction switching.Thus, the power source 602 supplies robust, reliable power to theaqueous reactor 601, preferably without requiring the use ofmetal-oxide-semiconductor field-effect transistors (MOSFETs) or otherdelicate switching devices. Preferably, an AC signal from thethree-phase alternator 610 is rectified using a three phase full waverectifier 612 to provide a DC drive output for the electrodes of thefield generator 603. A cooling device 615, for example a fan and coolingtower, is preferably connected across the drive output or to anotherpower source for cooling the alternator 610.

The apparatus 600 preferably further includes a vacuum pump 614 havingan inlet in fluid communication to an interior of the containment vesselfor the reactor 601, for example drawing from a head space 616 over thefield generator 601. A vacuum gauge 618 may be used to measure pressurein the reactor 601. For electrolysis of water, it has been founddesirable to maintain a vacuum in the head space 616 having a magnitudebelow that which would induce boiling or substantial production of vaporfor the operating temperature of the water. Some vacuum, one examplebeing run at about 0.5 atmospheres of vacuum, operates to initiate ormaintain a more robust electrolysis reaction, and create gas at lowertemperatures. The vacuum pump 614 is preferably also be used to draw offevolved gases from the reactor 601. Using an aqueous working fluid 620comprised of an electrolyte solution of a hydroxide salt in pure waterimmersing the field generator 603, the evolved gases in a non-separatedheadspace 616 should comprise about 60% molecular hydrogen, 30%molecular oxygen, and the balance water vapor or other impurities.Preferably, the evolved gases are passed through a heat exchanger 622 orcooler to cool and dry the gas before discharging for storage or enduse. A flow rate may be measured using any suitable flow meter 624.

Uses for a hydrogen and oxygen mixture may include mixing with otherfuels in a conventional hydrocarbon combustion engine to altercombustion conditions or emissions, or supplying as feedstock to achemical process to produce a product including but not limited topurified water. If the hydrogen is separated from the oxygen, theseparated hydrogen and oxygen may be provided to a proton exchangemembrane (PEM) fuel cell to produce electricity, for mobile orstationary applications. In addition, hydrogen may be combusted in ahydrogen combustion engine or gas turbine to produce electricity ormotive power. For example, hydrogen may be produced using renewableresources with variable duty cycles such as solar, wind or wave energy,and stored for combustion in a hydrogen engine or gas turbine for demandmatching purposes. The present technology is not limited to anyparticular end use for gases evolved from the reactor 601.

In alternative embodiments of an aqueous reactor 650 as shown in FIG.6B, one or more non-conductive barrier membranes 652 or diaphragms maybe disposed between at least two plates of the field generator 654between the anode plates and cathode plates, dividing the headspace 658into two or more compartments 660, 662. The barrier should extend belowthe fluid level and into the plate array of the field generator 654, butnot extend entirely through to the bottom of the array below the fluidlevel. The barrier may be placed roughly in the middle of the array orat other intermediate positions; for example, in a 25-plate array,between the 12.sup.th and 13.sup.th plates, or between the 13.sup.th and14.sup.th plates. A slot or other cutout may be made in the barrier toenable a jumper or electrical connector 664 connecting plates in aneutral subset of the array to pass through the barrier 652. Eachdivided part 660, 662 of the headspace may be evacuated in a separatestream. At low power, hydrogen should be concentrated in a compartment660 containing the cathode, and oxygen should be concentrated in acompartment 662 containing the anode.

In these alternative embodiments, it is advantageous to reduce the peakvoltage of the drive signal relative to embodiments wherein separationof hydrogen and oxygen is not performed. For example, for the examplereactor 650 configured as described herein with a single barrier 652, itmay be useful to reduce the voltage of the drive signal to somewhere inthe range of about 6 to 8 V to achieve better separation of hydrogen andoxygen. In such embodiments, gas bubbles are typically observed to formon plates located near the anode or cathode plates, but not onintermediate plates near the barrier 652. If an intermediate compartmentcontaining neither anode nor cathode is provided using two or morebarriers (not shown), it should contain a mixture of hydrogen andoxygen, which mixture may be separately evacuated.

Referring again to FIG. 6A, the apparatus 600 preferably furtherincludes a liquid pump 626 having an outlet coupled to a recirculationmanifold in the reactor 620. A recirculation manifold has been describedin connection with FIGS. 1 and 5 above. The recirculation manifold maybe positioned to direct one or more jets of recirculated working fluidbetween plates in the plate array of the field generator 603. The pump626 may also drive the recirculated working fluid through a heatexchanger 628 or other device for temperature control of the workingfluid. For various reactions, it may be advantageous to control thetemperature of the working fluid 620 to a set point, using a controlledheating or cooling process. For example, in an aqueous electrolysisprocess as described herein, it has been found advantageous to cool orheat the working fluid to maintain a temperature set point, depending onambient temperature or other factors. Higher concentrations ofelectrolyte may be advantageously employed as a function of sustainedlower temperatures.

The apparatus 600 preferably further includes a reservoir 630 ofdistilled water, and a control valve 632 for supplying make up water tothe reaction vessel to maintain a constant volume of working fluid 620during operation of the aqueous reactor 601. Although distilled waterwas used to prepare the working fluid, the present technology is notlimited to use of distilled water. For example, it may be possible toprepare a useable working fluid from filtered well water, or oceanwater. Using ocean water in a working fluid, it may be possible tooperate the aqueous reactor in a process for water distillation andpurification, by combusting the evolved hydrogen and oxygen to obtainpure water, with the heat of combustion being separately employed.

In accordance with the foregoing, a process 700 for disassociatinghydrogen and oxygen from water is depicted in FIG. 7. The process 700preferably includes immersing 702 a field generator, as describedherein, in an aqueous working fluid. The aqueous working fluid maycomprise or consist of a solution of a hydroxide salt in pure distilledwater or deionized water.

The method 700 preferably further includes supplying 704 electricalpower to one or more cathode plates and one or more anode plates atopposite ends of a field generator comprising an array of electricallyconductive parallel spaced-apart plates as described herein. The arrayof plates preferably includes a plurality of neutral plates interposedbetween the cathode plates and the anode plates of the types describedherein. The neutral plates are preferably arranged in interleavedneutral subsets each comprising at least three electrically connectedplates. Each of the neutral subsets may be electrically isolated fromother ones of the neutral subsets, from the cathode plates, and from theanode plates. For example, each of the neutral subsets may beelectrically isolated from every other one of the neutral subsets.

The method 700 preferably further includes disassociating 706 a fluidcomprising water disposed around the array of plates to evolvegaseous-phase hydrogen and oxygen, while supplying the electrical power.

In addition, FIG. 8 shows further optional operations 800 that may beimplemented for use in an apparatus performing the method 700. Theoperations 800 may be performed in any operative order; or performedconcurrently, partly or entirely, without requiring a particularchronological order of performance. Operations are independentlyperformed and not mutually exclusive. Therefore any one of suchoperations may be performed regardless of whether another downstream orupstream operation is performed. For example, if the method 700 includesat least one operation of FIG. 8, then the method 700 may terminateafter the at least one operation, without necessarily having to includeany subsequent downstream operation(s) that may be illustrated.

The operations 800 may include supplying the electrical power bysupplying 802 a direct current wave having a duty cycle in a range of10% to 90%, a frequency in a range of 500 Hz to 32 kHz, and morepreferably about 800 Hz, and a peak voltage in a range of 5 V to 50V.For example, duty cycles of 50% are believed advantageous. Frequency maybe tuned to maximize production for a given configuration of aqueousreactor, and are not limited to the stated range. Likewise, the peakvoltage may depend on the size and impedance of the reactor underoperating conditions. FIGS. 11, 12, 13, and 14 illustrate example signalresponses at test points TP1 and TP2 of FIG. 6B, wherein voltage isadjusted to pulses P of 15 volts at the desired frequency and dutycycle, which results in a measured current of about 70 amps to thereactor.

The operations 800 may include maintaining 804 a formulation of theworking fluid comprising a solution of a hydroxide salt in puredistilled water. In an embodiment, 120-220 grams, for example about 120grams, of KOH salt may be dissolved in 1.5 gallons of distilled water toprovide an initial volume of working fluid. The formulation may bemaintained by adding water to maintain a constant volume of workingfluid in the reaction vessel, during gas evolution. Reducing theconcentration of KOH (or other hydroxide salt) in the working fluidsubstantially below the stated range may reduce current flow through thefield generator & reduce the volume of gas evolved.

The operations 800 may include directing 806 at least one jet of fluidbetween ones of the plates in the array, for example using arecirculation manifold and pump as described above. The operations 800may include maintaining 808 the array of plates making up the fieldgenerator within a substantially sealed reaction vessel. In addition,the operations 800 may include maintaining 810 the array of plates atless than atmospheric pressure within the substantially sealed reactionvessel. For example, maintaining a vacuum pressure may include loweringan interior pressure of the substantially sealed reaction vessel to apressure in the range of about 0.3 to 0.8 atmospheres. For furtherexample, a vacuum of about 0.5 atmospheres may help initiate and sustaina robust generation of evolved gas from the field generator.

The operations 800 may include maintaining 812 a temperature of thefluid at a set point while disassociating the fluid. In an embodiment,the fluid may be initially at an ambient temperature that is above thefreezing point of the working fluid and below the boiling point of theworking fluid prior to operation, and maintained at or near a set pointof about 120.degree. F. during operation of the aqueous reactor.

The operations 800 may include removing 814 a mixture of the hydrogenand oxygen from the reaction vessel using a pump. In low powerembodiments, this may include removing a first stream comprisedprimarily of the hydrogen from a first portion of the reaction vesselproximal to the cathode plates and distal from the anode plates. In suchembodiments, removal may also include removing a second stream comprisedprimarily of the oxygen from a second portion of the reaction vesselproximal to the anode plates and distal from the cathode plates. Thisassumes that the first and second portions of the head space above thewater in the reaction vessel are separated by a non-conductive barriermembrane disposed between at least two plates of the array. In these andother embodiments, a mixture of hydrogen and oxygen may be withdrawntogether from a combined headspace.

When water is used without a carbon based material to create HHO, ashereinabove described, the temperature inside the aqueous reactor istypically observed to be between 115.degree. F. and 130.degree. F. Thevacuum inside the aqueous reactor 900 has been observed to vary up to1.5 atmospheres, with a typical observed magnitude of approximately 0.67to 0.8 atmospheres of vacuum at the beginning of the process andapproximately 0.33 to 0.5 atmospheres of vacuum when the process isoperating between 115.degree. to 130.degree. F. At steady state, thepower generating the field can be varied and the reactor cooled toachieve the appropriate temperature set point. In operation, theelectrical field inside the aqueous reactor is observed as beingsupplied with power at between 1 and 25 amps at between 12 and 24 volts.The power draw at the reactor 900 has been observed to be approximately6 to 6.5 amps at 12 to 14 volts. A similar output production of fuel canbe achieved by electrically connecting 4 reactors 900 in series andsupplying the reactors 900 with 2.4 amps at 12 volts as is producedusing one reactor 900 supplied with 6.5 amps of power at 12 volts. Foruse in a conventional engine application, it would be possible to createsufficient production of fuel from four reactors 900 so arranged cellsby supplying the necessary power from two alternators and two bridgeamplifying rectifier towers, each having a well-known conventionaldesign.

An alternative aspect of the technology is illustrated in FIG. 9. Inthis configuration, the technology utilizes an aqueous reactor 900 ofthe type hereinabove described, including a series of electrode platesets 902 a and b and an aqueous working fluid. The anode and cathodeplates for this process are preferably as described above andillustrated in FIG. 10, the representative plate 30, and can usecatalyst plated plates. The working fluid is preferably supplied to thereactor 900 as described above from a fluid tank 904, and preferablyuses de-ionized water. Where the aqueous working fluid also includes ahydrocarbon component, that component is preferably supplied from ahydro fuel tank 906. Preferably, the working fluid is a suspension of acarbon based material, such as a coal powder, mixed with one or moreliquid hydrocarbons and water as needed. The liquid hydrocarbon,preferably kerosene, diesel, or some other liquid hydrocarbon down toand including gasoline in molecular weight, is provided to help the coaldissolve more readily.

Where the technology utilizes a carbon based material, a hydro fuelmixer 908 is also provided to supply a mixture of liquid and carbonbased material to the aqueous reactor working. The hydro fuel tank 906preferably includes an agitator 908 to maintain the carbon basedmaterial in suspension in the fluid in the hydro fuel tank 906. In thepreferred embodiment, the carbon based material will be coal ground to afine powder having a median particle diameter of between 2 microns and50 microns, and preferably between 5 microns and 10 microns. Enhancedresults of the technology has been found to exist where the carbonpowder is produced through a turbine spun process or other process whichresults in the ground carbon particulates having an electrical charge.The hydro fuel tank 906 includes a drive motor 909 which will operatethe agitator 908 as necessary to maintain the carbon based materialparticulate in suspension in the liquid.

Preferably, upon initiation of the process, the aqueous reactor willcontain approximately two gallons of water, eight ounces of groundcarbon based material such as coal and four to six ounces of liquidhydrocarbon. Kerosene, diesel, or other liquid hydrocarbon down togasoline in molecular weight have been shown to work in the process. Theliquid hydrocarbon is mixed with the carbon material before introductionto the aqueous reactor. In the reactor, this range of mix appears tobetter reform with the disassociated hydrogen and oxygen present in theapplied electric field. Both the liquid hydrocarbon and the carbon basedmaterial are consumed in the presence of the disassociated elements ofelectrolysis. These ratios of ingredients in the aqueous reactor arecontrolled by supplying additional water from the water tank 904 oradditional liquid mixture of the hydrocarbons and suspended carbon basedmaterial from the hydro fuel tank 906 at the command of a controller910. In the preferred embodiment, as described above, the controller ispreferably a Mitsubishi FX3PLC which interfaces through a MitsubishiGT1055 user interface 911. The controller 910 also monitors the statusof the hydro tank 906 suspension and operates the drive motor 909 asneeded to maintain same.

The aqueous reactor preferably operates under an electrical fieldthrough the duty cycles described hereinabove, with fluid movementthrough the aqueous reactor 900 preferably enhanced, in the mannerhereinabove described and as illustrated in FIG. 9, through the use of acirculator pump 912 which is also controlled by controller 910. The fuelproduct of the aqueous reactor is evacuated from the reactor 900 by avacuum pump 920 through gas outlets 914 a, b.

In the preferred embodiment of the technology, the fuel product removedfrom the reactor 900 is passed through a dryer 916 to remove any liquidfrom the gas and through a flash suppressor 918 to minimize thepotential danger presented by the volatile fuel output from the reactor900. The technology also preferably includes other safety equipment suchas a burst chamber 922, designed to burst in the event of an explosion,and a series of check-valves 928 a, b, c to prevent any ignition sourcefrom reaching the aqueous reactor 900.

The fuel output of the reactor 900 can be used in a gaseous or liquefiedform. If the fuel is to be used in a gaseous form, the fuel gas isheated by a heat exchanger 924 and then passed through a descent filter926. It is thereafter supplied to a combustion chamber to serve as agaseous fuel. Alternatively, if the fuel gas is to be used as aliquefied fuel, the fuel gas is cooled by a chiller 925. It isthereafter supplied to a combustion chamber to serve as a liquid fuel.In either case, a needle valve (or a check valve with an appropriatepreselected pressure rating) 930 is interposed between the burst chamberand the chiller 925/heat exchanger 924 in order to control the pressure.The vacuum pump 920 and chiller 925 or heat exchange 924 are alsocontrolled by the main controller 910.

When a carbon based material and hydrocarbon fuel are added to theworking fluid in the aqueous reactor 900 using the technologyillustrated in FIG. 9 as outlined above, experimental results indicatethat the system can operate at 0.5 atmospheres of vacuum. In theoperating system, no vacuum or pressure is applied to the aqueousreactor 900. At the initiation of the aqueous reactor process,experimental results suggest that approximately 3.8 amps of power at 12volts is adequate to initiate the reaction in the reactor cell. Once thetemperature of the fluid inside the reactor reaches approximatelybetween 180.degree. F. and 200.degree. F., the power requirement hasbeen observed to reduce to approximately 2.8 amps at 12 volts. It isbelieved that plasma is formed inside the aqueous reactor that continuesto produce gaseous output for a time even after the electrical powerinput has been shut down until the plasma dissipates. At these levels ofproduction, the technology illustrated in FIG. 9 has been observed toconsume approximately 8 ounces of coal per hour.

Variations in the output of the technology illustrated in FIG. 9 can becontrolled by controlling the temperature and pressure inside theaqueous reactor, as well as the level and content of potassium hydroxideand/or the quantity of the chosen carbon based material fuel. Forexample, increasing the potassium hydroxide level in the reactor vesselwill draw additional power into the system, but can make the output lessproductive. The temperature of the working fluid is maintained within adefined range of between 180.degree. F. to 200.degree. F., using fluidrecirculation without pressure, to avoid the substantial production ofwater vapor or boiling. Under pressure, the upper end of the temperaturecan be raised accordingly and is believed to increase production.

For commercially productive units, it is believed that an aqueousreactor 900 that operates at approximately 2 bars and 300.degree. F.could be constructed to make commercial quantities of fuel using thetechnology illustrated in FIG. 9.

Other variations in the fuel output characteristics can be controlled bycontrolling other parameters, for example the pressure. It has beenobserved that higher pressure enhances the gas production from thetechnology illustrated in FIG. 9. The gas that is produced at higherpressures will tend to have a higher molecule count of hydrogen. Alighter fuel, however, can be produced by lowering the pressure insidethe reactor vessel. The technology illustrated in FIG. 9 is not limitedby or to any specific combination of temperature, pressure, electricalfield voltage and/or amperage, nor by any concentration of, the size of,or the choice of, any chosen carbon based material.

Example

Two 25-plate field generators each with stainless steel plates as shownin FIG. 3 were configured according to the topology shown in FIG. 2 in asealed reaction vessel, and connected in parallel to a power source. Avacuum pump was arranged to draw evolved gases from each vessel. Aworking fluid comprised of about 1.5 gallon of pure distilled water to120 grams of potassium hydroxide (KOH) salt was formulated and suppliedto each reaction vessel, immersing the field generators. No barrierdiaphragm was present. The vacuum pump was used to evacuate a headspaceof between about 3 to 4 inches in each aqueous reactor to about 7 inches(mercury) below atmospheric (i.e., 7 inches of vacuum), drawing about600 watts at 120 V. The temperature of the working fluid was maintainedat about 180.degree. F. using a recirculation pump drawing about 400watts at 220 V, passing the working fluid through a cooler anddischarging to recirculation manifold under the field generator, asdescribed. A square wave, 50% duty cycle DC input was supplied to thefield generators and resulted in maximum observed gas evolution at about15 V peak, drawing about 7.3 amperes. Pure distilled make up water wasadded to the aqueous reactors during gas evolution to maintain theliquid level in the reaction vessel. Very vigorous gas evolution wasobserved to occur uniformly on all plates in the field generator.Evolved gases were withdrawn from the headspace using the vacuum pump,which maintained a constant vacuum of about 7 inches Hg in the reactionvessel. Discharge from the vacuum pump was passed through a ball-floatflow meter and then discharged to the atmosphere. A sample of thedischarge was captured in a laboratory gas sample bag, and analyzedusing gas chromatography. A sample result of about 60% hydrogen, 30%oxygen was obtained. A total flow rate of about 100 L/min at standardtemperature and pressure (STP) was observed from combined discharge ofthe aqueous reactors, equivalent to about 60 L/min H.sub.2 or about ⅓ kgH.sub.2 per hour. A little more than three kilograms of water wereconsumed per hour by the apparatus, as would be expected given thelikely presence of some water vapor or condensed water in the discharge.

An alternative setup using a single gas barrier separating the anodeplates and cathode plates as shown in FIG. 6B was tested, with otherconditions as described in the foregoing paragraph. Initially, the DCinput voltage was adjusted to be about 12 Volts, and multiple voltagemeasurements during operated were taken at test points (TPs) identifiedin FIG. 6B for the anode, cathode, and neutral plates. At cathode TP(a)about 12 volts was measured repeatedly, wherein the word “about” is usedto mean plus or minus about 0.1 volts. The remaining TPs includedmeasurements of 11.3 volts at TP(b), 9.7 to 10.9 volts at TP(c), 8.1 to9.1 volts at TP(d), 6.5 to 7.3 volts at TP(e), about 5.5 volts at TP(f),3.2 to 3.6 volts at TP(g), 1.6 to 1.8 volts at TP(h), and zero volts atanode TP(i). However, the DC input voltage was further adjusted towithin the range of 6 to 8 volts, which increased gas volume generated.Under these conditions, a flow rate of about 40 L/min of gas wasobtained from the cathode side of the barrier, and a flow of about 20L/min of gas from the anode side. The gas obtained from the cathode sidewas observed to be combustible in air, but not explosive. The gasobtained from the anode side was not combustible. These observations areconsistent with production of separated hydrogen and oxygen gases fromopposite sides of the barrier.

Use of a catalyst such as platinum, palladium or nickel may be used toreduce the temperature for creating the plasma, there by reducing thetemp of the reformation of hydrocarbon into fuel.

In further examples, a reactor was configured similarly to the precedingexample to measure total input power, and wherein the working fluidcomprised a bath of about 3% KOH, and about 12 volts DC, 50% duty cycleat 800 Hz, was supplied to the reactor across the cathode and anode,with a 240 volt AC power supply drawing about 1.8 amps from an externalpower source. The vacuum pump was measured to draw about 2.3 amps froman external 120 volt AC power source. The reactor and vacuum pump powerinput was monitored continuously and were observed to draw a total of555.5 watts during operation.

During this example, water was hydrolyzed into hydrogen and oxygen gas(HHO) at a measured rate of 17.9 grams of water consumer per minute.Given that a mole of water has a mass of 18.0 grams, it follows that0.994 moles of water were generated per minute. Since an ideal gas has avolume of 22.4 liters per mole, it also follows that the reactorgenerated 0.994×22.4=22.26 liters per minute or 1335.6 liters per hourof HHO. If a mole of hydrogen is 1.0794 grams, and if1335.6×2/3/22.4=moles per hour of hydrogen are generated, this equatesto 39.75 grams per hour of generated hydrogen. Recalling that thereactor and vacuum pump consume 0.5555 kilowatts (Kw) to generate0.03975 kilograms (Kgs) in one hour, it follows that the reactorrequires about 13.97 KwH to generate one kilogram of hydrogen. At atypical off-peak rate of about $0.17 per KwH for external power, thereactor can generate hydrogen for about $2.37 per kilogram, which hasbeen found to be competitive.

The vacuum pump was used to evacuate a headspace of between about 3 to 4inches in each aqueous reactor to about 7 inches (mercury) belowatmospheric (i.e., 7 inches of vacuum), drawing about 600 watts at 120V. The temperature of the working fluid was maintained at about180.degree. F. using a recirculation pump drawing about 400 watts at 220V, passing the working fluid through a cooler and discharging torecirculation manifold under the field generator, as described. A squarewave, 50% duty cycle DC input was supplied to the field generators andresulted in maximum observed gas evolution at about 15 V peak, drawingabout 7.3 amperes.

Thus, an aqueous reactor and various uses of the reactor have beendisclosed. While embodiments and applications of this technology havebeen shown and described, it would be apparent to those skilled in theart that many more modifications are possible without departing from theinventive concepts herein. The invention therefore is not to berestricted except in the spirit of the appended claims.

What is claimed is:
 1. An apparatus for generating an electric field,comprising: one or more arrays of plates, the first array includingelectrically conductive parallel spaced-apart plates supported by anon-electrically conductive framework; wherein the first array of platesincludes one or more plates capable of being a cathode at a first end ofthe one or more arrays, one or more plates capable of being an anode ata second end of the one or more arrays opposite to the first end, andone or more neutral plates interposed between the plates capable ofbeing a cathode and an anode and electrically isolated from the cathodeplates and the anode plates; wherein a 3-phase full wave rectifier iscoupled with a 3-phase alternator having a field winding, to supply a DCdrive input to the cathodes and anodes; and wherein the 3-phasealternator is configured to be switched on and off at a frequency by adrive signal applied to the field winding such that a magnetic field isbuilt and collapsed according to the frequency.
 2. The apparatus ofclaim 1, wherein the plates of each array are interleaved with theplates of other of the arrays.
 3. The apparatus of claim 1, wherein theplates are substantially comprised of a material of high conductivityplated with a catalyst interactive in electrolysis.
 4. The apparatus ofclaim 3, wherein the interactive catalyst is nickel.
 5. The apparatus ofclaim 1, wherein the anode and cathode plates have a pattern of holesthere through; and wherein the nominal sizes of the plates are similarand the area of the pattern of holes on each anode and cathode plate isgreater than the remaining solid area of each anode and cathode plate.6. The apparatus of claim 1, further comprising: a source of appliedelectrical power connected to the cathode plates and to the anode platesand including a waveform generator; and wherein the waveform generatorproduces the drive signal to have a duty cycle in a range of 10% to 90%,a frequency in a range of 800 Hz to 32 kHz and a peak voltage in a rangeof 5 V to 50V.
 7. The apparatus of claim 1, further comprising anon-conductive barrier membrane disposed between the anode and thecathode plates to prevent gasses from comingling above the water.
 8. Aprocess for disassociating hydrogen and oxygen from water in a reactionvessel, comprising: supplying electrical power to one or more cathodeplates and one or more anode plates at opposite ends of one or morearrays of electrically conductive parallel spaced-apart plates;supplying the electrical power as a DC drive input from a 3-phase fullwave rectifier coupled with a 3-phase alternator having a field windingand wherein the 3-phase alternator is configured to be switched on andoff at a frequency by a drive signal applied to the field winding suchthat a magnetic field is built and collapsed according to the frequency;wherein the array of plates comprises a plurality of neutral platesinterposed between the cathode plates and the anode plates; anddisassociating water containing an electrolyte disposed around the arrayof plates to evolve gaseous-phase hydrogen and oxygen, while supplyingthe electrical power.
 9. The process of claim 8, wherein supplying theelectrical power further comprises supplying the drive signal to have aduty cycle in a range of 10% to 90%, a frequency in a range of 800 Hz to32 kHz and a peak voltage in a range of 5 V to 50V.
 10. The process ofclaim 8, further comprising maintaining a temperature of the water in arange of about 115.degree. F. to 130.degree. F. and under a vacuum belowthe boiling point of the water while disassociating the water.
 11. Aprocess for preparing a combustible fluid, comprising: providing aliquid fuel stock including a suspension of carbon based material inwater with an electrolyte having: one or more cathode plates and one ormore anode plates at opposite ends of one or more arrays of electricallyconductive parallel spaced-apart plates that further include neutralplates interposed between and electrically isolated from the cathodeplates and the anode plates; applying an electric current by a provided3-phase full wave rectifier that is coupled with a 3-phase alternatorhaving a field winding and wherein the 3-phase alternator is configuredto be switched on and off at a frequency by a drive signal applied tothe field winding such that a magnetic field is built and collapsedaccording to the frequency, to supply a DC drive input across thecathode and anode plates to generate a combustible gaseous output fromthe liquid fuel stock; and extracting the combustible gaseous outputfrom the reaction vessel.
 12. The process of claim 11, wherein thecarbon based material has an electrical charge prior to being suspendedwithin the water.
 13. The process of claim 11, wherein the carbon basedmaterial includes coal having a median particle diameter of not largerthan approximately 10 microns.
 14. The process of claim 11, whereinapplying the electrical power further comprises supplying the drivesignal to have a duty cycle in a range of 10% to 90%, a frequency in arange of 80 Hz to 32 kHz and a peak voltage in a range of 5 V to 50V.15. The process of claim 11, wherein the liquid fuel stock is maintainedat a temperature of approximately 180.degree. F. or above during theapplication of said current and under sufficient pressure to maintainthe liquid fuel stock below a boiling point of the water whilegenerating the combustible gaseous output.
 16. The process of claim 11,wherein the liquid fuel stock further includes liquid hydrocarbon fuel.17. The process of claim 16, wherein the volumetric ratio of hydrocarbonliquid to carbon base material is from about 0.75 to one to about one toone.